Apparatus for the manufacture of gas.



PATENTED DEC. 20, 1904.

H. S. ELWORTHY. APPARATUS FOB. THE MANUFACTURE OP GAS.

APPLICATION FILED JAN. 21, 1903.

3 SHEETS-SHEET 1.

N0 MODEL W/T/VESSES:

vPATENTED DEG. zo. 1904.

H. S. ELWOR'IHY. APPARATUS FOR THE MANUFAGTURE OE' GAS.

APPLICATION FILED JAN. 21, 1903.

3 SHEETS-SHEET 2.

N0 MODEL.

gm 23m w r/vf 5515s- No. 777,848. PATENTED DEG. 20, 1904.

` H. S. ELWORTHY.

APPARATUS FOR THE MANUFAGTURE 0F GAS.

APPLIGMION FILED JAN. 21, 1903. No MODEL. a snnms-smm s.

cin/M passing such Patented December 20, 1904.

HERBERT SAMUEL ELVVORTHY, OF LONDON, ENGLAND, ASSIGNOR OF ONE-HALF TOERNEST HENRY ENGLAND.

WILLIAMSON, OF LONDON,

APPARATUS FOR THE IVIANUFACTURE OF GAS,

SPECIFICATION forming part of Letters Patent No. 777,848, dated December20, 1904.

Application filed Ianuary 21, 1903. Serial No. 139,941.

To @ZZ whom, it 711,013/ concern:

Be it known that I, HERBERT SAMUEL EL- WORTHY, consulting chemicalengineer, of Dashwood House, New Broad street, London, England, haveinvented certain new and useful Improvements Relating to the Manufactureof Gas for Illuminating, Heating, and Power Purposes, of which thefollowing is a specification.

This invention relates to the manufacture of a gas consisting chiefly ofmethane or marshgas. y

It is well known that the ordinary coal-gas of commerce owes its highcaloriiic value to the presence of methane, which usually forms aboutthirty per cent. of that product. Natural4 gas, the high calorific valueof which is so well known, frequently consists almost entirely ofmethane.

By the present invention I am enabled to manufacture a gas consistingchieiiy of methane from water-gas by iirst forming a suitable mixture ofcarbon monoxid, carbon dioxid, and hydrogen, or a mixture of hydrogenwith either one of theabove oxids of carbon (adding hydrogen wherenecessary) and then mixture of gases over iinely-divided nickel at asuitable temperature. I prefer to obtain this mixture of oxid or oxidsof carbon and hydrogen by the process hereinafter described. In general,however, I prefer to proceed in the manner first to be detailed, thoughI do not coniine myself to this particular method.

Methane consists of hydrogen and carbon in the proportions representedby the formula CIL, In order, therefore, to obtain this gas, it isnecessary to have a suiiicicnt quantity of hydrogen present in themixture not only to combine with the carbon to form the methane, butalso to combine with the oxygen liberated from its combination with 'thecarbon.

Water-gas made in the ordinary way consists principally of a mixture ofcarbon monoxid and hydrogen in nearly equal volumes, together with asmall quantity of nitrogen and carbon dioxid. Now for my purpose itisnecessary to have about three volumes of hydrol l l gen to one volume ofcarbon monoxid in order to obtain the reaction represented by theequation If, however, the water-gas is so made as to consist largely ofcarbon dioxid and hydrogen, then it is necessary to have about fourvolumes of hydrogen to one volume of carbon dioxid in accordance withthe equation In the method of manufacturing water-gas generally adoptedit is essential to raise the proportion of carbon monoxid to thelhighest limit obtainable and to keep down the proportion of carbondioxid to the lowest limit. For the purpose of my invention, however,this is more or less a matter of indifference, as I can utilize the oneas well as the other. Therefore, while in the ordinary well-knownprocess of water-gas manufacture (except in the case of theDellwik-Fleischer process) the blowing method is generally twice aslong, at least, as the steaming process, in the case of my invention thesteaming period may be very considerably increased, and consequently afar greater quantity of water-gas obtained at each reversal, therebyeffecting a very great saving of fuel now lost during the prolongedblowingup periods. Having obtained the water-gas,

conveniently this modified water-gas, I proceed to secure the necessaryquantity of hydrogen to bring` up the proportions to those stated above,according to the composition of the water-gas mixture. In order to dothis, I may obtain my hydrogen by any of the wellknown processes, as byelectrolysis ofA water, in which case the oxygen may be collected forcommercial use; but I prefer to obtain it by the reaction of steam uponmetallic iron, whereby at a suitable temperature the steam isdecomposed, the hydrogen liberated, and the iron converted to the stateof magnetic oxid in accordance with the equation.

I preferably effect the production of the hydrogen required foradmixture with the water-gas, as above mentioned, by the action of steamon iron in a more economical manner than has hitherto been known. This Ieffect by storing up the heat produced in one part of thehydrogen-making processfnamely, the reduction to the metallic state ofthe magnetic oxid of iron produced during the hydrogenmaking stage-and Ithus render that heat available to assist in the carrying out of thatreaction. I may effect this by placing the metallic iron or iron oxid inthe form of powder on trays in a suitable furnace, said trays beingformed of fire-clay and acting in the same manner as the ordinaryfire-brick filling used in the Cowper or VVhitwell regenerative stoves.In this way great economy results, and the iron being in the form of afine powder is readily acted upon in both stages. Neither does itdeteriorate in the same way as when iron ore or iron scraps are used, asfurnaces in which these latter are used tend to close up from formationof the powdered oxid. In the improved furnace this powder is anadvantage, whereas in other forms it is a disadvantage. The fire-bricktrays are or may be of rectangular shape, havinga retaining-rib at twoor more of their edges for containing the powder and mounted on shortlegs or supports. They are built up one upon another in the furnace insuch manner as to allow the gases to pass freely, but by a circuitouspathway, through the furnace. The furnace is preferably heatedinternally, and to this end it may be also so constructed with acombustion-chamber in the base that it can in the first place be heatedto the required extent by gas-firing either with producer, water, orcoal gas. It may, however, be constructed without thiscombustion-chamber in the base and heated by means of hot air or heatedproducts of combustion from another' source, preferably by a hot-airblast from an ordinary regenerative stove, and this stove may be the onein which the steam which has to be passed over the iron for theproduction of hydrogen is superheated at a later stage, as hereinafterdescribed. I may also arrange the iron-furnace so that it can be heatedinternally both by gas-firing and by hot blast of air or heated productsof combustion. In order to facilitate the production of the hydrogen bycontact of steam with iron, a reaction in which a considerableabsorption of heat takes place in addition to heating thc retorts orfurnaces containing the iron the steam used for the reaction may be veryhighly superheated in regenerative blaststoves, such as the wellknownCowper or VVhitwell stoves so largely used in the iron industry, or inan apparatus such as described in English Patent No. 25,007 of 1897. Theiron should be in a finely-divided state,but may i be in porous lumps,if desired. In order to reduce the oxid of iron to the metallic state,and thus render it available for reuse, I may pass a certain quantity ofthe producer-gas made during the blowing-up stage of the water-gasprocess or in other convenient way over it at a high temperature,whereby the carbon monoxid contained in that gas, assisted by the smallproportion of hydrogen generally present, reduces it in accordance withthe equation the hydrogen being at the same time converted into water.gas for the reduction of the iron, it is advisable to superheat theproducer-gas, as in this manner greater heat is produced and stored upin the iron-containing furnace for use in the hydrogen-making part ofthe process. The carbonio acid made in this reduction of the iron oxidby producer-gas can, if required, be collected and further purified byany suitable process, such as absorption by carbonated alkalies eitherin the moist state or in solution, and finally recovered from these byboiling the solution or passing su- Aperheated steam over the moistbicarbonate.

Instead of using the producer-gas for reducing the oxid of iron I mayuse a portion of the water-gas or the gas from a separate gasproducerpreferably worked by means ofa steam jet-blower, as a certain proportionof hydrogen assists in the reduction of the iron oxid by the carbonmonoxid.

The hydrogen having been mixed with the water-gas in suitableproportion, as before mentioned, and assuming the watergas to containboth oxids of carbon, I proceed to pass this mixture of gases overfinely-divided nickel, whereby the carbon ishydrogenized and the oxygenliberated is converted into water by the excess of hydrogen present. Thenickel apparently takes no part in the reaction, as at the end of theoperation it remains unaltered, the reaction belonging apparently to theso-called catalytic or contact order. It is probable,however,that at anintermediate stage the reaction discovered by Ludwig Mond takesplace-viz., the production of nickel carbonyl-but this will beimmediately decomposed by the comparatively high temperature at whichthe process is worked. Although iron also forms a compound with carbonmonoxid in a similar manner to nickel, it does not appear to have thepower of hydrogenizing the carbon. The nickel may simply be placed inlayers in the powdered state upon suitably-arranged shelves in theretort, chamber, or other vessel, or it may be caused to adhere to thesurface of some porous material, as broken fire-brick, pumice-stone, orasbestos liber, an agglutinating and not easily fusible substance beingused-such as pipe-clay, fire-clay, magnesium chlorid, or other suitablematerialor the finely -divided nickel itself may be made up into ballsor blocks of any suitable size by being mixed with an agglutinating ma-When using producer-V IOO IIO

terial and preferably, also, with some organic material, such assawdust, which can easily be burned away, leaving the blocks moreporous, or the nickel may be in the form of wire gauze or foil or othersuitable form, so as to present a large surface to the gases. Thefinely-divided nickel as produced by the Mond reaction is especiallysuitable for the purposes of this invention. The nickel, howeverprepared, is placed in a retort, tower, or chamber, which may be heatedinternally or externally by any suitable means to the requiredtemperature-say, for example, 250O centigrade for the carbon monoxid and550O for the dioxid-and the gases may also be heated before admission tothe chamber. Instead of heating the chamber itself the gases beforeadmission may be heated to the required temperature, and I prefer thismethod because in this manner the reaction is more under control, ashotter or colder gas can be admitted at any stage of the reaction, so asto control the temperature. The reaction is strongly exothermic, and itis therefore advisable to be able to readily control the temperature,because should the temperature rise too high the monoxid will bedecomposed into carbon and not converted into methane. I may control thetemperature, as before described, by admitting the reaction-gases at ahigher or lower temperature, as required, or with the same object I mayadmit to the nickel-chamber at any suitable stage a certain volume ofsteam orwater spray, or it may be a certain volume of cold methane. Ifsteam be employed, it can be condensed,.so that the resulting methanewill not be contaminated thereby, or with the same object ofcontrolling' the temperature of the reaction I may circulate a definitevolume of water or cold air or other gas through Coils of pipe in thechamber or in a hollow casing surrounding said chamber, or it may bethrough hollow shelves, upon which the nickel rests. As the temperatureof the reaction with carbon monoxid is lower than the reaction withcarbon dioxid, the process may be conducted in two stages, the firststage at the lower temperature to convert the carbon monoxid to methaneand the latter stage at a higher temperature in order to convert thecarbon dioxid to the methane, and the gases may be reheated during theintermediate stage. The two stages are preferably conducted in separatechambers. The methane is collected in a gas-holder for use.

There are several modifications which may be adopted, if desired, undercertain circumstances. By suitable steaming during the water-gasprocess-21e., by stopping the steamingI at the required point-a gashaving approximately the composition CO2+CO+3H2 may be obtained, andfrom this the carbon dioxid maybe removed by any well-known method, suchas those detailed below, though I do not confine myself to these. Afterthe removal of the carbon dioxid the mixture of carbon monoxid andhydrogen is in the right proportion for the production of methane. Anyof the following methods may be used for the removal of the carbondioxid:

First. It may be passed over slaked lime, whereby carbonate of lime isproduced, and the lime may be reviviiied by any process, such asHislops. f

Second. The gases may be passed over an alkaline carbonate or through asolution of these salts, and the carbonio acid may be recovered from themoist salts by passing superheated steam over them, or it may berecovered from the solution by boiling. In either case the monocarbonateis regenerated and the carbon dioxid recovered in a very pure state andsuitable for commercial utilization when compressed to the liquid stateor solidified, as may be done bythe process described under EnglishPatent No. 7,436 of 1895. In the solid state the carbonio acid will haveimportant uses for refrigeration, &c.

Third. Tlie carbon dioxid may be removed from the mixed gases byabsorption in water.

This may be done in the manner described in the specification of EnglishPatent No. 7,281 of 1895, which is a continuous process, or it may beremoved by compressing the gas alternately into two vessels connected bymeans of a three-way valve, these vessels being fitted with agitatingdevices, and the compressed mixture of gases is forced into one end ofthe vessel, the carbon dioxid absorbed during its passage to the otherend, and the insoluble hydrogen and carbon monoxid escaping through asuitable valve at the opposite end, where they are collected andconveyed toa storageholder. Vhen the pressure in the vessel reaches aset limit, such as five to ten atmospheres, the three-way valve isautomatically reversed and the compressed gases pass into the othervessel. At the same time the outlet-valve for the insoluble gases isclosed and an escape-valve for the carbon dioxid opened, and this israpidly given off from the water as the pressure is lowered, while thisliberation is facilitated by the agitation being con- 'tinued.

The CO2 so liberated may be collected for use and may be furtherpurified from the remaining traces of hydrogen and carbon monoxid bypassing over copper oxid, as fully described in the specification ofEnglish Patent No. 25,007 of 1897.

Instead of manufacturing the water-gas in the ordinary manner, asdescribed above, when a very pure methane free from nitrogen is requiredthe water-gas may be made in thc manner fully detailed in thespecification of English Patent No. 25,007 of 1897, above nientioned, inwhich the steam is superheated to such a degree, by passing' throughmodilied Cowper or IVhitwell stoves, that on coming in contact with thefuel it is decomposed IOO IIO

into carbon monoxid, carbon dioxid, and hydrogen.

1t may be advisable after a certain time to revivify the nickel, andthis may be done by passing air at a high temperature over it to oxidizethe metal and then reducing it by means of hydrogen, or instead of thisprocess the method of convertingit into nickel-carbonyl by passing COover it at a lower' temperature may be used, the nickel liquid compoundpassing away into another chamber or retort, where it is decomposed byraising the temperature, and the CO liberated can be used over again tovolatilize a further quantity of nickel.

There are various economies which may be introduced at different stagesof the process in order to save otherwise waste products. During theblowing-up stage of the water-gas part of the process a very largequantity of producer-gas is generated,and that part of it which is notrequired for the reduction of the iron oxid, where the iron process ofhydrogen production is used, may be utilized either for steam raising'or, preferably, for driving gasengines of the type now coming so largelyinto use in England and on the Continent for working with the wastegases from the blastfurnaces in the iron and steel industry, many ofthese engines now being made to deliver fifteen hundred to two thousandhorse power. The power so obtained may be utilized in any manner, as forthe production of electricity, and this latter may be used for anycommercial purposesuch as driving machinery,

, electrochemical processes, lighting, or for the decomposition of waterfor the production of hydrogen and oxygen;the former of which may beutilized in my process and the latter collected and used for anycommercial purpose. XV here the'process of separating the carbonic acidby absorption is used, the power generated in the above manner may beused for compressing the mixed gases and also for liquefying thepurified carbonio acid obtained in any of the processes detailedhereinbefore. rlhe producer-gas may also be utilized for the heating ofthe regenerative stoves, as mentioned above, which stoves may be usedfor super-heating the steam used in various parts of the process andalso for heating the mixed gases before passing them lover the nickel.Both the producr-gas and the water-gas may also be caused to pass directfrom the producer through any suitable form of heat-interchanger inwhich its sensible heat is given up, and this heat may be used for anyrequired purpose. Should a process for making the water-gas similar tothe Dellwik- Fleischer process be used, in which practically noproducer-gas is made, the heated products of combustion, as well as thehot-water gas, may be used either by means of a heatinterchang ingdevice or for steam raising' or su perheating.

Another method of working the water-gas part of the process andobtaining the requisite proportion of hydrogen is as follows: Bycarrying on the steaming part of the water-gas process until the gas hasapproximately the composition'QCO-l-GOz-l-LHQ a mixture is obtainedwhich'when the CO is removed will be in the right proportion forproducing the methane. In order to do this, lmake use of the Mondreaction by passing the mixed gases at a suitable temperature over thefinely-divided nickel, thus combining the CO with the nickel in the formof the liquid known as nickel-carbonyl, the CO2 and hydrogen passing onand being carried over a further quantity of nickel at a highertemperature. The nickel-carbonyl is itself decomposed by slightlyraising its temperature, metallic nickel and carbon monoxid beingreproduced. rlhe recovered carbon monoxid can be used in any requiredway, such as mixing it with the methane in the proportion allowed by lawor using it for fuel or for power production by means of gas-engines. Itmay also be mixed with the producer-gas formed during the blowing-upstage in order to increase its fuel value or caloritic power. rlhismethod also provides a ready means of revivifying the nickel when itspower of catalytic action is exhausted.

lnstead of simply heating the nickel-carbonyl to decompose it intometallic nickel and carbon monoxid, as just described, I may mix thesaid nickel-carbonyl with a suitable proportion of hydrogen gas,obtained in the particular manner hereinbefore described or in any othersuitable way, and pass said mixture through a heated chamber orotherwise subject it to a suitable temperature to cause such mixture ofhydrogen and nickel-carbonyl to be transformed, substantially, intometallic nickel, methane, and water. A suitable proportion of hydrogenfor this purpose would be approximately twelve volumes for each volumeof the nickel-carbonyl, and a suitable temperature for the reactionwould be about 250O centigrade. It will be readily understood that thehydrogen` may be admitted at the required temperature to thenickel-carbonyl, and a special heating-chamber may thus be dispensedwith.

The accompanying drawings illustrate apparatus embodying the presentinvention and suitable for the production of a gas consisting largely ofmethane from water-gas, as above described, taking as examples themethods hereinbefore described in which a water-gas is producedconsisting, substantially, of a mixture of monoxid and dioxid of carbonand hydrogen, the dioxid being either removed or not and hydrogen beingadded, necessary, to bring the proportion thereof up to that necessaryto substantially transform the oxid or oxids of carbon into methane andwater.

rl`he practical application of the invention as regards the othermodifications above de- IOO IlO

ethe solution of scribed will then be readily understood by thoseskilled in the art.

In the drawings, Figure 1 is a diagrammatic view of a plant suitable forcarrying out the invention as before mentioned. Fig. 2 is a sectionalside elevation, on an enlarged scale,of the improved hyd regen-producerconstructed to embody the improvements hereinbefore described, a few ofthe end trays being shown in section. Fig. 3 is a sectional frontelevation of the hydrogenproducer, partly in transverse verticalsection, on the line A B of Fig. 2.

l is the water-gas producer, which may be of any ordinary or suitableconstruction. 2 is the steam-inlet thereto; 3, the air-blower,delivering the air-blast thereto, when required, by the inlet 4.

5 is a condenser through which the waterl gas passes on leaving theproducer 1, a regulating-valve 6 being interposed to open, close, orregulate the iiow of gas, as required.

7 is a pipe leading from the condenser, and 8 is a blower for drawing'the gaseous mixture from the condenser and forcing it through thesystem.

13 is a three-way cock whereby the gaseous mixture may be directedthrough the pipe 7a to the carbon-dioxid absorber 9 or led by the pipe10 direct to the pipe 24 beyond the absorber 9, according as it isdesired to remove the carbon dioxid from the gaseous mixture or not. Thecarbon-dioxid absorber is shown as of cylindrical form with domed ends.It is provided at bottom with a perforated false bottom or grid 11, uponwhich is supported a suiiicient depth of broken lire-brick, cokebreeze,or the like 12. Vhen the cock 13 is turned to direct the gases to theabsorber, they are delivered by the blower 8, through the pipe 7, to thespace 9xL below the false bottom 11 and rise up through the materialthereon.

14 is a spraying-head attached toa pipe 15 and serving' to spray asolution of carbonate of potash upon the surface of the coke or. othermaterial in the absorber. The pipe 15 leads from the casing of aheat-interchanger 16, containing a coil 17, the upper end of which leadsby a pipe 18 to a boiler 19, the pipe 18 dipping down to near the bottomof said boiler. Another pipe,20,leads from the top of the casing of theheat-interchanger 16 to the top of the boiler 19. The bottom of the coil17 communicates,by a pipe 21,with the chamber 9a of the absorber 9, acirculating-pump 22 being interposed between the coil 17 and saidabsorber. The pump 22 serves to draw bicarbonate of potash resultingfrom the absorption of the carbonic acid by the carbonate of potashsolution from the bottom of the absorber 9 and delivers it through thepipe 21, coil 17, and pipe 18 to the boiler 19, where the carbon dioxidis driven ofi" by the heat of the furnace and passes away from the crownof the boiler by a pipe 23 to a suitable gas-holder or other apparatusfor use as and when required The regenerated carbonate-of-potashsolution passes from the top of the boiler, by the pipe 20, through thecasing of the heat-interchanger 16, where it heats up the cool solutionin the coil 17, being itself cooled by the incoming bicarbonateof-potashsolution, and passes by the pipe 15 to the top of the absorber 9, whereitis sprayed over the coke or lire-brick filling by the spraying-head14. In this way a solution of carbonate of potash is continuouslydelivered to the absorber, where it meets the gaseous mixture andabsorbs the carbon dioxid therefrom, the resulting solution ofbicarbonate being passed through the heat-interchanger to the boiler,sothat the dioxid is usefully recovered and the heat is advantageouslyeconomized.

24 is a pipe to which the gaseous mixture passes from the top of theabsorber 9, (or direct by the pipes 7 and 10, as the case may be.) 25 isthe hydrogen-producer. (Shown in detail in Figs. 2 and 3 and more fullyhereinafter described.) 26 is a pipe leadingfrom the upper part thereof,by which the hydrogen generated passes to the mixing-chamber 27, intowhich the pipe 24 likewise delivers, so as to effect the properadmixture of the gases therein. A regulating-valve 27 is interposed inthe pipe 26 to permit the supply of hydrogen to be regulated, so as toadjust the hydrogen in the ultimate mixture to the -desired proportion,as before explained, or to allow of the hydrogen being shut off when itis not required to mix the samewith the gases passing to the nickelchamber or chambers or for other purpose, as required. The mixingchamber27fL is connected to a coil or serpentine 24, arranged in a superheater28, arranged to be heated by gaseous or solid fuel, as desired, andprovided with suitable valves or equivalent means for regulating thetemperature. In its passage through this coil or serpentine the gaseousmixture is heated to the proper temperature to insure the desiredreaction between said mixture and the nickel in the nickel-chamber whenit is delivered thereto. From the coil or serpentine 24a the mixturepasses, by a pipe 29, to the nickelchamber 30. rlhe nickel-chamber is ofrectangular form and is shown as constructed with an air-casing 31,through which air may be circulated by a pump 32, when required, so asto control the temperature within said chamber. The nickel (in any ofthe forms hereinbefore described) is carried on trays 33, superposed inbailed order in the chamber in such manner that the gaseous mixturepasses up in a serpentine course over each of the trays successivelyfrom bottom to top and is brought into intimate contact with the nickelthereon. The methane produced in the nickel-chamber 30 passes 01T fromthe top of said chamber at 33, whence it may be led to a gas-holder, or

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when a mixture of carbon monoxid, carbon dioxid, and hydrogen isemployed in the reaction the resulting mixture of methane, carbondioxid, and hydrogen is preferably led through a second superheater 28and a second nickel-chamber 30", similar to those just described, beforepassing to the gas-holder.

Let us assume, by way of example, that itis desired to produce awater-gas consisting, substantially, of carbon monoxid, carbon dioxid,and hydrogen, wherein the monoxid and hydrogen are present in suchproportion that on removal of the dioxid the monoxid and hydrogen shallremain in suflicient proportion for their substantial transformation inthe nickelchamber into methane and water, as before explained. Theworking of the apparatus will then be as follows: As the water-gas isproduced in the producer 1 the valve 6 is opened, three-way valve 13 isturned to direct the gases to the absorber 9, the regulatingvalve 27 isclosed, and the blower 8 and circulating-punipV 22 are set in operation.rJfhe mixture of hydrogen, carbon monoxid, and carbon dioxid is drawn bythe blower through the condenser 5 and delivered to the absorber 9,rising through the coke or {ire-brick and the descending stream ofcarbonate-of-potash solution therein, whereby the carbon dioxid isabsorbed. The remaining gases then pass through the coil or serpentinein the superheater 28, the temperature in the superheater beingregulated to heat said gases to the proper temperature for the monoxidreaction-for example, 2500 centigrade. The gases then pass to thenickel-chamber 30, where they are transformed into methane and steam,the mixture of methane being passed through a condenser, (not shown,)where the steam is condensed, and the methane then passes to thegas-holder, as above explained. Should the temperature in thenickel-chamber rise too high, this is rectified by pumping air throughthe casing 31 'or spraying water into said casing or in other suitableway. Itis of advantage to maintain the temperature in the chamber bythis means at or slightly above that necessary for the reaction.

Let us assume another case-namely, that in which water-gas consisting,substantially, of carbon monoxid, carbon dioxid, and hydrogen isproduced, additional hydrogen being` then mixed therewith to bring thehydrogen up to the proper proportion, the resulting mixture being causedto react with the nickel to produce methane. In this case the apparatuswould be operated as follows: Cock 6 is opened, three-way valve 13turned to pass the gaseous mixture from the condenser to pipe 24 direct,and regulating-valve 27 adjusted to deliver the hydrogen to themixingchamber 27 in proper proportion. rllhe blower' 8 is set inoperation, but the circulating-pump 22 is of course not run. The mixtureof gases passes through the coil in the superheater 28,

the heat wherein is regulated to a suitable temperature for the monoxid.rl`hence they pass to the nickel-chamber 30, where the monoxid and partof the hydrogen are converted into methane and water. The resultingmixture of gases then passes through the coil or serpentine in thesecond superheater 28, the heat of which is adjusted to a suitabletemperature to insure the reaction of the carbon dioxid and hydrogensay350O centigrade -and the gases thus heated are passed through the secondnickel-chamber 30 and thence through a condenser to the gas-holder, asbefore, the temperature in the nickel-chambers being kept within theproper limits, as before described. In any case, as will be readilyunderstood, hydrogen can be admitted by the regulating-valve 27 to themixingchamber 27 as and when required to bring the hydrogen content ofthe gaseous mixture up to the proportion required for the reaction.

I will now proceed to describe the improved hydrogen-producer asillustrated in the drawings. This producer consists of a rectangularstructure of refractory brick, with an outer metallic shell or casingand having an arched top, as shown. It is formed or provided at the basewith inlet 34 for gaseous fuel for heating up the generator whenrequired and. also with another inlet, 35, for producer or water gas forreducing the oxid of iron formed in the hydrogen-producing reaction,both these inlets being provided with suitable valves 34SL 35, Fig. 1,to enable them to be closed. 1t will be obvious that one such inletwould sufiice; but it is in many cases convenient to have separateinlets for the heating and reducing operations. On the iioor 36 of thegenerator I dispose a convenient number of pillars or supports 37, thesebeing arranged at equal distances apart along and across the base of thegenerator, so as to support the ends of the trays for containing ironwhen these are superposed thereon, as described later. Acombustion-chamber 38 is thus provided at the base of the generator.Avalved air-inlet 39 opens through the side of the generator into thecombustion-chamber 38, andasteam-'inlet pipe 40, Fig. 1, is alsoarranged to discharge into same.

40 isa manhole for cleaning purposes provided with a suitable door.

41 represents the trays for containing the iron. lrlhese are ofrefractory fire-brick. They are of square shape in plan and are of formin section, as seen in Fig. 3-that is to say, they are formed with aiiange or lip at two opposite sides extending for a short distance aboveand below the central horizontal plane of the tray, so as to support theflanges of the tray next above and provide a channel betweeneaeh pair ofsuperposed trays for the passage of the steam or gases. These trays arefilled with iron in powdered form and are piled one above another alongand across the generator, the abutting corners or angles of IOO lIO

the bottom range of trays being supported by the pillars 37 disposed, asbefore described, at equal distances along and across the floor of theproducer. The remaining trays are built up over the bottom range oftrays, each range being supported by the lianges of the trays of the rownext below. The refractory fire-brick lining at the right and left handside of the generator is formed with a vertical series ofsupporting-ledges 42, extending from front to back, each of these ledgesbeing designed to support the end trays of the range next above at theside Where the particular ledge is situated. Each range of trays isdisposed in baffled or staggered order with respect to the range nextabove it, the left-hand trays of the bottom row, for example, beingsupported on the bottom left-hand ledge 42 and lying close against thewall ofthe generator, while the right-hand trays of the bottom range donot extend quite to the wall on the right-hand side. (See Fig. 2.) Therighthand end trays of the second range are then supported on the bottomright-hand support 42 and similarly lie close against the wall at thatside, while the left-hand trays of this second range do not extend quiteto the opposite wall, and so on to the top, this arrangement beingadopted to allow for expansion of the trays when heated. The end traysof each range, which are supported by the ledges 42, are somewhatdifferent in shape from the other trays. Their form will be seen onreference to Fig. 2, which shows some of these end trays in section. Itwill be seen that the flanges or lips of these trays are curved toconform to the curve of the supporting-ledges, and at the side adjacentthereto they are formed with a lip 41, extending from front to back ofthe tray, so that when each range of trays is placed in position theheating or reducing gases or steam, as the case may be, passed throughthe generator is or are baiiied. by every succeeding range of trays ateach side of the generator alternately, so that the steam or gases passfrom the top of each range of trays to the top of the range next above,so as to pass over the material on same, as shown by the arrows, Figs. 2and 3. Further, the abutting lips or flanges of the trays, which'arebuilt up, as before described, constitute vertical walls or partitionswhich divide the interior of the generator up into a number ofindependent flues or passages running in a zig- Zag course from back tofront and from front to back alternately from bottom to top of thegenerator. of the steam or gases with the material on each tray isassured, and, moreover, the large quantities of heat evolved in thereaction of the producer-gas with the iron to reduce the oxid of iron isstored up and rendered available for use in the oxidation stage of theworking, great economy being thus attained. Each range or course oftrays is also preferably disln this way intimate contact posed inslightly-staggered order with respect to the range next above, as shownin Fig. 3, a slight space being' left between the end trays of eachrange at the front and back alternately. In this way the trays canexpand evenly without interfering with uninterrupted course of thegases, as above described.

43 is the hydrogen-outlet to the supplypipe 26.

44 is an outlet-pipe for the waste gases obtained in the reducing stageof the workingthat is to say, when producer or other reducing gas ispassed through the generator to reduce the iron oxid formed in thehydrogenproducing stage. A valve 45 is provided in the outlet-pipe 44 toenable this to be opened and closed when required.

46 is a manhole adapted to be closed by a suitable door and givingaccess to the interior of the generator to enable the trays to be placedin position therein.

It will be understood that when the generator is lirst run to producehydrogen the trays contain a suitable depth of metallic iron infinely-divided form and are' piled up in position, as above explained. Aconvenient way of obtaining the finely-divided metallic iron is to fillthe trays with oxid ofy iron and pile them in position in the furnaceand then reduce the oxid to the metallic state by passing producer orwater gas over it after it has been heated to the required temperature.When the iron is in the metallic state, valves 34a 45 and airinlet 39are opened and the manholes, inlet 35, and valve 27 are closer.Tater-gas or other gaseous fuel at a high temperature is admitted by theinlet 34. The gaseous fuel on meeting' the air in the base of thegenerator is ignited and the hot products of combustion rise through thetrays, thus heating them to a high temperature, the heat being absorbedand stored by the lire-brick trays and filling. Then the interior of thegenerator has thus been heated to a sufficient temperature, the gasinlet34, air-inlet 39, and valve 45 are closed and valve 27 is opened. Steam,preferably superheated, is turned on by the pipe 40 and circulatesaround the trays, oxidizing the iron thereon, the resulting hydrogenpassing away by the pipe 26. In order to revivify the iron, valve 27,inlet 34, and air-inlet 39 are closed and valve 45 is opened. Produceror water gas is then admitted by inlet 35 and in its IOO TIO

passage around the trays reduces the iron oxid thereon, the waste gasespassing away to a chimney or uptake by the valve 45. vIf necesssary, thegenerator may be heated up in the manner above described before passinggas therethrough to the producer or water revivify the iron.

I make no claim in the present application to the process of gasmanufacture hereinbefore described, as such process forms the subject ofLetters Patent No. 7 38,303, dated September 8, 1903, issued to ErnestHenry Wil- IZO liamson and myself, nor do 1 make any claim l in thepresent application to the specifical form or embodiment ofhydrogen-generator herein described, this forming the subject of anapplication for patent divisional hereof and filed on March 21, 1904,Serial No. 199,130.

`What 1 claim, and' desire to secure by Letters Patent, is

1. An apparatus for the mannfacture of gas suitable for illuminating,heating or power purposes, comprising', in combination,

(a) a water-gas plant, (2)) a plant for the production of hydrogen gas,(c) a conversion-chamber for combining said gases in contact withnickel, and (d) suitable connections between said plants and saidconversion-chamber,and means for regulating the operation of said plantsand chamber.

2. An apparatus for the manufacture of gas suitable for illuminating,heating or power purposes, comprising, in combination, (a) a water-gasplant, (b) means for removing an oxid of carbon from water-gas, (c) aconversionchamber for combining water-gas with hydrogen in contact withnickel, (d suitable connections and means for regulating the operationof said parts, and (e) means for introducing hydrogen into saidconversion-chamber.

3. An apparatus for the manufacture of gas suitable for illuminating,heating or powei' purposes, comprising, in combination, (a) a water-gasplant, (b) means for absorbing said carbon dioxid from water-gas, (c) aconversionchamber for combining water-gas with hydrogen in contact withnickel, (d) suitable connections and means for regulating the operationof said parts, and (e) means for introducing hydrogen into saidconversion-chamber.

4. An apparatus for the manufacture of gas suitable for illuminating,heating or powei' purposes, comprising, in combination, (a) a water-gasplant, (7)) a chamber arranged to be heated and to facilitate thepassing of steam over iron to produce hydrogen, means for passing adeoXidiZing-gas through said chamber, (d) a conversion-chamber forcombining said water-gas and hydrogen in contact with nickel, and (e)suitable connections and means for regulating the operation of saidparts.

5. An apparatus for the manufacture of gas suitable for illuminating,heating or power purposes, comprising, in combination, a water-gasproducer, a condenser connected thereto, a carbon-dioxid absorber,connected to said condenser, means for delivering acarbon-dioXid-absorbing solution to said absorber, a heat-interchanger,a boiler wherein said solution can be regenerated by driving oif by heatthe carbon dioXid absorbed thereby in the absorber, conduits betweensaid absorber and said h eat-interchanger and between said boiler andsaid interchanger whereby said absorbent solution can be delivered fromsaid boiler through said heat-interchanger to said absorber and theregenerated solution delivered from the absorber through saidintel-changer to the boiler, means for so delivering the absorbentsolution to said boiler and said absorber, a conduit at the deliveryside of said absorber, a hydrogen-generator, a hydrogen pipe orconnection connecting said hydrogengenerator to said last-mentionedconduit whereby hydrogen may be caused to miX with the gases issuingfrom the absorber, a heater through which the conduit at the deliveryside of the absorber passes at a point beyond its junction with thehydrogen pipe or connection, a nickelconversion chamber into which saidlast-mentioned conduit delivers,

said chamber containing metallic nickel, all substantially as described.

6. An apparatus for the manufacture of gas suitable for illuminating,heating or power purposes comprising, in combination, a watergasproducer, a condenser connected thereto a carbon-dioxid absorber,connected to said condenser, means for delivering acarbon-dioxidabsorbing solution to said absorber, a heatinterchanger, aboiler wherein said solution can be regenerated by driving off by heatthe carbon dioXid absorbed thereby in the absorber, conduits betweensaid absorber and said heat-interchanger and between said boiler andsaid interchanger whereby said absorbent solution can be delivered fromsaid boiler through said heat-interchanger to said absorber and theregenerated solution delivered from the absorber through saidinterchanger to the boiler, means for so delivering the absorbentsolution to said boiler and said absorber, a conduit at the deliveryside of said absorber, a heater through which the conduit at thedelivery side of the absorber passes, a nickel-conversion chamber intowhich said last-mentioned conduit delivers, said chamber containingmetallic nickel, all substantially as described.

7 An apparatus for the manufacture of gas suitable for illuminating,heating or power purposes,comprising, in combination,a watergasproducer, a condenser connected thereto, a conduit at the delivery sideof said condenser, a hydrogen-producer, a hydrogen pipe or connectionconnecting said hydrogen-producer to said conduit whereby hydrogen maybe caused to mix with the gases issuing from the condenser, a heaterthrough which said conduit passes at a point beyond its junction withthe hydrogen pipe or connection and a nickelconversion chamber to whichsaid conduit delivers, said chamber containing metallic nickel allsubstantially as described.

8. An apparatus for the manufacture of gas suitable for illuminating,heating or power purposes, comprising, in combination, (a) a water-gasplant, (L) a plant for producing hydrogen gas, (c) a conversion-chamberfor combining the carbon monoXid of said water-gas with hydrogen incontact with nickel, (d) a second conversion chamber for converting IOGthe carbon dioxid of said water-gas with hydrogen in Contact withnickel, and (e) suitable connections and means for regulating theoperation of said parts.

9. An apparatus for themanufacture of gas suitable for illuminating,heating or power purposes,comprising, in combination, a watergasproducer, a condenser connected thereto, a conduit at the delivery sideof said condenser, a hydrogen-producer, a hydrogen pipe or connectionconnecting said hydrogen-producer to said conduit whereby hydrogen maybe caused to mix with the gases issuing from the condenser, a heaterthrough which said conduit passes at a point beyond its junction withthe hydrogen pipe or connection and a nickel-con- HERBERT SAMUELELWORTHY.

Witnesses:

WALTER J. SKERTEN, GEO. J. B. FRANKLIN.

